US4133662A - Production of high pressure oxygen - Google Patents

Production of high pressure oxygen Download PDF

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US4133662A
US4133662A US05/751,453 US75145376A US4133662A US 4133662 A US4133662 A US 4133662A US 75145376 A US75145376 A US 75145376A US 4133662 A US4133662 A US 4133662A
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Norbert Wagner
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Linde GmbH
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Linde GmbH
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    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04151—Purification and (pre-)cooling of the feed air; recuperative heat-exchange with product streams
    • F25J3/04187—Cooling of the purified feed air by recuperative heat-exchange; Heat-exchange with product streams
    • F25J3/04218—Parallel arrangement of the main heat exchange line in cores having different functions, e.g. in low pressure and high pressure cores
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
    • F25J3/04012—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of warm gaseous streams; details of intake or interstage cooling
    • F25J3/04024—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of warm gaseous streams; details of intake or interstage cooling of purified feed air, so-called boosted air
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
    • F25J3/04078—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression
    • F25J3/0409—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression of oxygen
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
    • F25J3/04078—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression
    • F25J3/04103—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression using solely hydrostatic liquid head
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04151—Purification and (pre-)cooling of the feed air; recuperative heat-exchange with product streams
    • F25J3/04187—Cooling of the purified feed air by recuperative heat-exchange; Heat-exchange with product streams
    • F25J3/04193—Division of the main heat exchange line in consecutive sections having different functions
    • F25J3/04206—Division of the main heat exchange line in consecutive sections having different functions including a so-called "auxiliary vaporiser" for vaporising and producing a gaseous product
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
    • F25J3/04284—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams
    • F25J3/0429—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams of feed air, e.g. used as waste or product air or expanded into an auxiliary column
    • F25J3/04303—Lachmann expansion, i.e. expanded into oxygen producing or low pressure column
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
    • F25J3/04284—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams
    • F25J3/04309—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams of nitrogen
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
    • F25J3/04375—Details relating to the work expansion, e.g. process parameter etc.
    • F25J3/04381—Details relating to the work expansion, e.g. process parameter etc. using work extraction by mechanical coupling of compression and expansion so-called companders
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04406—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using a dual pressure main column system
    • F25J3/04412—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using a dual pressure main column system in a classical double column flowsheet, i.e. with thermal coupling by a main reboiler-condenser in the bottom of low pressure respectively top of high pressure column
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2205/00—Processes or apparatus using other separation and/or other processing means
    • F25J2205/24—Processes or apparatus using other separation and/or other processing means using regenerators, cold accumulators or reversible heat exchangers
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2250/00—Details related to the use of reboiler-condensers
    • F25J2250/30—External or auxiliary boiler-condenser in general, e.g. without a specified fluid or one fluid is not a primary air component or an intermediate fluid
    • F25J2250/40—One fluid being air
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2250/00—Details related to the use of reboiler-condensers
    • F25J2250/30—External or auxiliary boiler-condenser in general, e.g. without a specified fluid or one fluid is not a primary air component or an intermediate fluid
    • F25J2250/50—One fluid being oxygen

Definitions

  • This invention relates to a system for the separation of air by two-stage low-temperature rectification wherein the air is subjected to a preliminary purification step, compressed, and cooled by heat exchange with separation products.
  • the oxygen product of the low pressure stage is generally evaporated in indirect heat exchange contact with condensing nitrogen of the high pressure stage.
  • the relationship of the pressures of the two rectification stages is based on the requirement that the condensation temperature of the nitrogen must be somewhat above the vaporization temperature of the oxygen. Due to this thermodynamic correlation between the pressure conditions in both stages, the pressure of the high pressure stage is clearly dependent on the desired pressure of the products withdrawn from the low pressure stage. Consequently, if it is desired to obtain the separation products at higher pressures, the pressure of the high pressure stage must also be raised, and, therefore, the entire air feed must be compressed to a higher pressure. This results in high operating costs, particularly in the case of large-scale plants.
  • a principal object of this invention is to develop a generally improved air separation process, and especially for the production of relatively high pressure oxygen.
  • relatively high pressure is meant about at least 1.6 bars, preferably at least 1.8 bars, and particularly in the range of about 1.7 to 3.6 bars.
  • a process is provided wherein a portion, e.g. 18 to 34, preferably 24 to 28% of the feed air is further compressed in a recompressor prior to the cooling thereof and is at least partially liquefied in a condenser-evaporator in heat exchange with evaporating product oxygen before being introduced into the rectifying column.
  • the feed air from the main compressor is at a pressure of about 5.8 to 7.8 bars, preferably about 6.2 to 6.8 bars; absolute accordingly, in the recompressor the air is compressed from such pressures to the pressure necessary to obtain the desired pressure of oxygen product.
  • the air in the recompressor is usually compressed from the pressure of the main compressor to about a pressure of about 6.5 to 10 bars preferably 7.2 to 8.0 absolute bars. In any case, the recompressor will compress the air incrementally at least 0.7, preferably 1.0 to 2.2 bars.
  • the air is usually liquefied to the extent of at least 70%, preferably at least 80%, and particularly in the range of 75 to 100%.
  • the product oxygen can now be obtained under a pressure higher than that of the low pressure stage. This is possible, because according to the invention a portion of the higher-compressed, condensing feed air now yields the heat of vaporization for the oxygen.
  • the pressure in the oxygen vapor space of the condenser-evaporator can be increased by arranging the condenser-evaporator at a lower level than the sump of the low pressure column, thereby imposing a "column of oxygen” additional pressure on the vapor space. It is likewise possible to provide an increased pressure in the oxygen vapor space of the condenser-evaporator by a liquid pump, with the aid of which the liquid product oxygen is pumped from the sump of the low pressure column into the condenser-evaporator. In general, the pressure in the oxygen vapor space of the condenser-evaporator is maintained at about 0.4 to 2.0, preferably 0.6 to 1.0 bars higher than the pressure in the sump of the low pressure column.
  • the process of this invention can also be utilized with special advantage in air separation plants containing a compensating stream which is engine-expanded in a turbine.
  • the compensating stream can be nitrogen as well as air. It was found that, in this method, the energy produced at the expansion turbine frequently cannot be exploited economically, since the conversion into electrical energy is economically, since the conversion into electrical energyd is economically ineffecient and unattractive. Therefore, it is particularly advantageous to utilize the mecahnical energy obtained at the expansion turbine directly for the further compression of the portion of the feed air according to this invention.
  • For additional details of processes employing a compensating stream attention is invited to, for example, R. E. Latimer "Distillation of Air" Chem. Engineering Progress Feb. 1967 p. 35/59
  • regenerators as opposed to reversible heat exchangers, are employed on account of their long lifetime and reliable operation.
  • they have the disadvantage that the product oxygen must be warmed in very expensive tubular coils within the regenerators.
  • it has been proposed to warm the product oxygen agains a portion of the feed air in a separate heat exchanger, but in this case, the air must be cleaned in a molecular sieve system prior to entering the heat exchanger.
  • the recompressed portion of the feed air is now cleansed in a molecular sieve system before being cooled in heat exchange with product oxygen.
  • FIG. 1 is a schematic diagram of a preferred embodiment of an air separation plant according to the invention with a reversing exchanger as the primary heat exchanger, wherein nitrogen is utilized as the compensating stream; and
  • FIG. 2 is a schematic flowsheet of a system as illustrated in FIG. 1 with the preferred aspect of the invention wherein regenerators serve as the primary heat exchangers and with molecular sieves for cleaning a portion of the air. Air is utilized as the compensating stream.
  • a system according to this invention consists of a revex 1 or a pair of regenerators 1", a twin rectifying column consisting of a high pressure column 2 and a low pressure column 3, a condenser-evaporator 4, a recompressor 5, and an expansion turbine 6.
  • the conventional devices for switching the flow paths in the reversing exchanger are not illustrated, since this would obfuscate the drawing.
  • the regenerator pair is shown only as a single heat exchanger, in correspondence with its function.
  • Preliminary purified and compressed air at a pressure of 6.5 bars is subdivided into two partial streams at point 7 (FIG. 1).
  • the larger (74%) of the two partial streams is cooled in reversing exchanger 1 to 102° K. and introduced into the high pressure column 2 at point 20.
  • Crude fractions of oxygen and nitrogen are withdrawn via conduits 8 and 9, respectively, from the high pressure column 2, cooled in heat exchanger 10, expanded in valves 11 and 12, respectively, and introduced into the low pressure column for purposes of further rectification.
  • Residual gas is withdrawn from the head of the low pressure column 3 via conduit 13; after the residual gas has been warmed in heat exchangers 10 and 1, it leaves the plant.
  • Gaseous nitrogen is withdrawn from the head of the high pressure stage 2 at point 14 and, in order to maintain the desired, small temperature difference, introduced into the reversing exchangers 1 and 1' at the cold ends thereof. Before the heat exchange process is terminated, this stream is again withdrawn from reversing exchangers 1 and 1' and, after engine expansion in turbine 6, admixed to the residual gas withdrawn via conduit 13, which leaves the plant by way of reversing exchangers 1 and 1'.
  • product oxygen is withdrawn in the liquid phase from the low pressure column 3 via conduit 15 at a pressure, e.g., of 1.5 bars and vaporized in condenser-evaporator 4 at a pressure of, e.g., 2.4 bars before being withdrawn from the plant via conduit 16 by way of revex's 1 and 1'. Due to the fact that the condenser-evaporator is located at a higher level, the pressure in the oxygen vapor space is increased by the hydrostatic pressure of the feed conduit 15. If product oxygen is desired which is under an even higher pressure, than a liquid pump can be connected into the feed conduit 15 in the evaporation space of the condenser-evaporator 4 to provide an additional pressure increase.
  • a liquid pump can be connected into the feed conduit 15 in the evaporation space of the condenser-evaporator 4 to provide an additional pressure increase.
  • the amount of heat required for vaporization is supplied by the minor partial air stream branched off at point 7, this stream being further compressed, in accordance with the invention, in recompressor 5, to e.g., 7.4 bars and is cooled in reversing exchanger 1'.
  • This partial air stream is condensed in the condenser-evaporator 4 against evaporating product oxygen and then introduced into the high pressure column 2. Due to the fact that the product oxygen is vaporized in indirect heat exchange contact with air, which is under a higher pressure as compared to the high pressure column, this product oxygen itself can also be obtained under a higher pressure.
  • a pair of regenerators 1" serves as the primary heat exchanger.
  • the air, further compressed in recompressor 5 according to this invention, is purified in a molecular sieve system 17 before being cooled in heat exchange with product oxygen in heat exchanger 18.
  • the nature of the molcular sieve is that it removes undesired impurities from the air, i.e. H 2 O, CO 2 , C 2 H 2 , C 2 H 6 , C 3 H 6 , C 4 H 8 , to an extent of 99.95%.
  • the preliminary purification removes H 2 O, CO 2 , C 4 H 8 to an extent of 99.7%.
  • These undesired impurities are deposited in liquid or solid form within the passages of the reversing heat exchanger as the air is passed over the cold surface. They are removed when the passages are switched on to low pressure waste service.
  • the driving force to remove the solid contaminants from the heat exchanger surface comes from the difference in vapor pressure between the high pressure and low pressure streams.
  • a pump 21 is provided for transferring and increasing the pressure of the oxygen product from the low pressure column to the condenser-evaporator.

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  • Engineering & Computer Science (AREA)
  • Physics & Mathematics (AREA)
  • Mechanical Engineering (AREA)
  • Thermal Sciences (AREA)
  • General Engineering & Computer Science (AREA)
  • Health & Medical Sciences (AREA)
  • Emergency Medicine (AREA)
  • Separation By Low-Temperature Treatments (AREA)
US05/751,453 1975-12-19 1976-12-16 Production of high pressure oxygen Expired - Lifetime US4133662A (en)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE2557453A DE2557453C2 (de) 1975-12-19 1975-12-19 Verfahren zur Gewinnung von gasförmigem Sauerstoff
DE2557453 1975-12-19

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US4133662A true US4133662A (en) 1979-01-09

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US (1) US4133662A (enExample)
JP (1) JPS5289565A (enExample)
AU (1) AU500646B2 (enExample)
BR (1) BR7608165A (enExample)
DE (1) DE2557453C2 (enExample)
FR (1) FR2335809A1 (enExample)
GB (1) GB1511977A (enExample)
ZA (1) ZA761237B (enExample)

Cited By (22)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4560398A (en) * 1984-07-06 1985-12-24 Union Carbide Corporation Air separation process to produce elevated pressure oxygen
WO1986006462A1 (en) * 1985-04-29 1986-11-06 Erickson Donald C Increased argon recovery from air distillation
US4895583A (en) * 1989-01-12 1990-01-23 The Boc Group, Inc. Apparatus and method for separating air
US5036672A (en) * 1989-02-23 1991-08-06 Linde Aktiengesellschaft Process and apparatus for air fractionation by rectification
US5082482A (en) * 1989-10-09 1992-01-21 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Process and apparatus for the production of gaseous oxygen with a variable flow by air distillation
US5265429A (en) * 1992-02-21 1993-11-30 Praxair Technology, Inc. Cryogenic air separation system for producing gaseous oxygen
US5363657A (en) * 1993-05-13 1994-11-15 The Boc Group, Inc. Single column process and apparatus for producing oxygen at above-atmospheric pressure
US5410885A (en) * 1993-08-09 1995-05-02 Smolarek; James Cryogenic rectification system for lower pressure operation
US5526647A (en) * 1994-07-29 1996-06-18 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Process and installation for the production of gaseous oxygen under pressure at a variable flow rate
US5560223A (en) * 1994-10-25 1996-10-01 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Process and installation for the expansion and compression of at least one gaseous stream
EP0756143A1 (en) * 1995-07-28 1997-01-29 The Boc Group, Inc. Adsorption process with high and low pressure feed streams
US5794458A (en) * 1997-01-30 1998-08-18 The Boc Group, Inc. Method and apparatus for producing gaseous oxygen
US5802872A (en) * 1997-07-30 1998-09-08 Praxair Technology, Inc. Cryogenic air separation with combined prepurifier and regenerators
US5839296A (en) * 1997-09-09 1998-11-24 Praxair Technology, Inc. High pressure, improved efficiency cryogenic rectification system for low purity oxygen production
US5901579A (en) * 1998-04-03 1999-05-11 Praxair Technology, Inc. Cryogenic air separation system with integrated machine compression
US5924307A (en) * 1997-05-19 1999-07-20 Praxair Technology, Inc. Turbine/motor (generator) driven booster compressor
EP1319912A1 (de) * 2001-12-14 2003-06-18 Linde Aktiengesellschaft Vorrichtung und Verfahren zur Erzeugung gasförmigen Sauerstoffs unter erhöhtem Druck
CN104445076A (zh) * 2013-09-12 2015-03-25 气体产品与化学公司 用于生产臭氧和氧的集成的方法
US20190368811A1 (en) * 2018-05-31 2019-12-05 Air Products And Chemicals, Inc. Process and Apparatus for Separating Air Using a Split Heat Exchanger
US20220252345A1 (en) * 2019-04-05 2022-08-11 Linde Gmbh Method for operating a heat exchanger, arrangement with a heat exchanger, and system with a corresponding arrangement
EP4163576A1 (en) * 2021-10-06 2023-04-12 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Apparatus and process for the separation of air by cryogenic distillation
TWI909227B (zh) 2022-10-18 2025-12-21 美商氣體產品及化學品股份公司 用於分離包含氧、氮及氬之一饋料氣體之製程及其分離系統及一種改造一空氣分離單元之方法

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DE2854508C2 (de) * 1978-12-16 1981-12-03 Linde Ag, 6200 Wiesbaden Verfahren und Vorrichtung zur Tieftemperaturzerlegung eines Gasgemisches
FR2461906A1 (fr) * 1979-07-20 1981-02-06 Air Liquide Procede et installation cryogeniques de separation d'air avec production d'oxygene sous haute pression
DE3016317A1 (de) * 1980-04-28 1981-10-29 Messer Griesheim Gmbh, 6000 Frankfurt Verfahren zur gewinnung von fluessigen stickstoff
EP0093448B1 (de) * 1982-05-03 1986-10-15 Linde Aktiengesellschaft Verfahren und Vorrichtung zur Gewinnung von gasförmigem Sauerstoff unter erhöhtem Druck
GB2125949B (en) * 1982-08-24 1985-09-11 Air Prod & Chem Plant for producing gaseous oxygen
DE3307181A1 (de) * 1983-03-01 1984-09-06 Linde Ag, 6200 Wiesbaden Verfahren und vorrichtung zur zerlegung von luft
JPS61259077A (ja) * 1986-05-08 1986-11-17 株式会社神戸製鋼所 空気分離方法
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US4560398A (en) * 1984-07-06 1985-12-24 Union Carbide Corporation Air separation process to produce elevated pressure oxygen
WO1986006462A1 (en) * 1985-04-29 1986-11-06 Erickson Donald C Increased argon recovery from air distillation
US4670031A (en) * 1985-04-29 1987-06-02 Erickson Donald C Increased argon recovery from air distillation
US4895583A (en) * 1989-01-12 1990-01-23 The Boc Group, Inc. Apparatus and method for separating air
US5036672A (en) * 1989-02-23 1991-08-06 Linde Aktiengesellschaft Process and apparatus for air fractionation by rectification
AU625950B2 (en) * 1989-10-09 1992-07-16 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Process and apparatus for the production of gaseous oxygen with a variable flow by air distillation
US5082482A (en) * 1989-10-09 1992-01-21 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Process and apparatus for the production of gaseous oxygen with a variable flow by air distillation
US5265429A (en) * 1992-02-21 1993-11-30 Praxair Technology, Inc. Cryogenic air separation system for producing gaseous oxygen
US5363657A (en) * 1993-05-13 1994-11-15 The Boc Group, Inc. Single column process and apparatus for producing oxygen at above-atmospheric pressure
US5410885A (en) * 1993-08-09 1995-05-02 Smolarek; James Cryogenic rectification system for lower pressure operation
US5526647A (en) * 1994-07-29 1996-06-18 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Process and installation for the production of gaseous oxygen under pressure at a variable flow rate
US5560223A (en) * 1994-10-25 1996-10-01 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Process and installation for the expansion and compression of at least one gaseous stream
EP0756143A1 (en) * 1995-07-28 1997-01-29 The Boc Group, Inc. Adsorption process with high and low pressure feed streams
US5794458A (en) * 1997-01-30 1998-08-18 The Boc Group, Inc. Method and apparatus for producing gaseous oxygen
US5924307A (en) * 1997-05-19 1999-07-20 Praxair Technology, Inc. Turbine/motor (generator) driven booster compressor
US5802872A (en) * 1997-07-30 1998-09-08 Praxair Technology, Inc. Cryogenic air separation with combined prepurifier and regenerators
US5839296A (en) * 1997-09-09 1998-11-24 Praxair Technology, Inc. High pressure, improved efficiency cryogenic rectification system for low purity oxygen production
US5901579A (en) * 1998-04-03 1999-05-11 Praxair Technology, Inc. Cryogenic air separation system with integrated machine compression
EP1319912A1 (de) * 2001-12-14 2003-06-18 Linde Aktiengesellschaft Vorrichtung und Verfahren zur Erzeugung gasförmigen Sauerstoffs unter erhöhtem Druck
EP1319913A1 (de) * 2001-12-14 2003-06-18 Linde AG Vorrichtung und Verfahren zur Erzeugung gasförmigen Sauerstoffs unter erhöhtem Druck
CN104445076A (zh) * 2013-09-12 2015-03-25 气体产品与化学公司 用于生产臭氧和氧的集成的方法
US9371228B2 (en) 2013-09-12 2016-06-21 Air Products And Chemicals, Inc. Integrated process for production of ozone and oxygen
US20190368811A1 (en) * 2018-05-31 2019-12-05 Air Products And Chemicals, Inc. Process and Apparatus for Separating Air Using a Split Heat Exchanger
CN110553466A (zh) * 2018-05-31 2019-12-10 气体产品与化学公司 使用分裂热交换器来分离空气的方法和设备
EP3575717A3 (en) * 2018-05-31 2020-03-11 Air Products And Chemicals, Inc. Process and apparatus for separating air using a split main heat exchanger
US11054182B2 (en) * 2018-05-31 2021-07-06 Air Products And Chemicals, Inc. Process and apparatus for separating air using a split heat exchanger
CN110553466B (zh) * 2018-05-31 2021-08-06 气体产品与化学公司 使用分裂热交换器来分离空气的方法和设备
US20220252345A1 (en) * 2019-04-05 2022-08-11 Linde Gmbh Method for operating a heat exchanger, arrangement with a heat exchanger, and system with a corresponding arrangement
US12044471B2 (en) * 2019-04-05 2024-07-23 Linde Gmbh Method for operating a heat exchanger, arrangement with a heat exchanger, and system with a corresponding arrangement
EP4163576A1 (en) * 2021-10-06 2023-04-12 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Apparatus and process for the separation of air by cryogenic distillation
TWI909227B (zh) 2022-10-18 2025-12-21 美商氣體產品及化學品股份公司 用於分離包含氧、氮及氬之一饋料氣體之製程及其分離系統及一種改造一空氣分離單元之方法

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JPS5289565A (en) 1977-07-27
FR2335809A1 (fr) 1977-07-15
DE2557453C2 (de) 1982-08-12
DE2557453A1 (de) 1977-06-30
JPS5634784B2 (enExample) 1981-08-12
BR7608165A (pt) 1977-11-22
AU2021676A (en) 1978-06-08
FR2335809B1 (enExample) 1982-09-10
GB1511977A (en) 1978-05-24
AU500646B2 (en) 1979-05-31
ZA761237B (en) 1977-02-23

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